NO144711B - PROCEDURE FOR BLACKING OXYGEN-EQUIVALIZED CELLULOSE-containing OZONE - Google Patents
PROCEDURE FOR BLACKING OXYGEN-EQUIVALIZED CELLULOSE-containing OZONE Download PDFInfo
- Publication number
- NO144711B NO144711B NO781190A NO781190A NO144711B NO 144711 B NO144711 B NO 144711B NO 781190 A NO781190 A NO 781190A NO 781190 A NO781190 A NO 781190A NO 144711 B NO144711 B NO 144711B
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- Prior art keywords
- ozone
- peroxide
- bleaching
- oxygen
- pulp
- Prior art date
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims description 31
- 238000000034 method Methods 0.000 title claims description 26
- 229920002678 cellulose Polymers 0.000 title description 4
- 239000001913 cellulose Substances 0.000 title description 4
- 238000004061 bleaching Methods 0.000 claims description 25
- 150000002978 peroxides Chemical class 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 239000000126 substance Substances 0.000 claims description 12
- 230000002378 acidificating effect Effects 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 5
- 238000010979 pH adjustment Methods 0.000 claims description 5
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 claims description 5
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 5
- 238000003825 pressing Methods 0.000 claims description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 21
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 description 10
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 8
- QPCDCPDFJACHGM-UHFFFAOYSA-N N,N-bis{2-[bis(carboxymethyl)amino]ethyl}glycine Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(=O)O)CCN(CC(O)=O)CC(O)=O QPCDCPDFJACHGM-UHFFFAOYSA-N 0.000 description 8
- 239000000460 chlorine Substances 0.000 description 8
- 229910052801 chlorine Inorganic materials 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 6
- 239000004155 Chlorine dioxide Substances 0.000 description 5
- 235000019398 chlorine dioxide Nutrition 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 239000007844 bleaching agent Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical class [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000005660 chlorination reaction Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 238000006385 ozonation reaction Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- NGNBDVOYPDDBFK-UHFFFAOYSA-N 2-[2,4-di(pentan-2-yl)phenoxy]acetyl chloride Chemical class CCCC(C)C1=CC=C(OCC(Cl)=O)C(C(C)CCC)=C1 NGNBDVOYPDDBFK-UHFFFAOYSA-N 0.000 description 1
- 244000166124 Eucalyptus globulus Species 0.000 description 1
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 1
- 235000011613 Pinus brutia Nutrition 0.000 description 1
- 241000018646 Pinus brutia Species 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000006353 environmental stress Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000005286 illumination Methods 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 235000012254 magnesium hydroxide Nutrition 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000004045 organic chlorine compounds Chemical class 0.000 description 1
- 150000004965 peroxy acids Chemical class 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000005070 ripening Effects 0.000 description 1
- 239000011780 sodium chloride Chemical class 0.000 description 1
- 239000011122 softwood Substances 0.000 description 1
Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
- D21C9/1057—Multistage, with compounds cited in more than one sub-group D21C9/10, D21C9/12, D21C9/16
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Paper (AREA)
- Polysaccharides And Polysaccharide Derivatives (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
- Compositions Of Macromolecular Compounds (AREA)
Description
Den foreliggende oppfinnelse vedrører en fremgangsmåte til bleking av oksygendelignifiserte celluloseholdige masser, oppslemmet i vann, såsom sulfat-, soda-, og sulfittmasser med et tørrstoffinnhold større enn 15%, med ozon i et surt miljø The present invention relates to a method for bleaching oxygen-delignified cellulosic masses, suspended in water, such as sulphate, soda and sulphite masses with a dry matter content greater than 15%, with ozone in an acidic environment
og peroksyd, idet ozonbehandlingen finner sted i to trinn. and peroxide, as the ozone treatment takes place in two stages.
Vanlige blekningsprosesser innbefatter ved fremstilling av fullstendig blekede masser (hvithetsgrad = 88% MGO), et eller to kloreringstrinn med elementær klor, og i de fleste tilfeller dessuten et eller to hypoklorittrinn og et eller to klordioksydtrinn. I kloreringstrinnet hvor der vanligvis benyttes 4-8% CI2beregnet på mengden av masse, dannes der store mengder saltsyre, hvilket medfører at bakvannet inne-holder store mengder av denne syre respektive natriumklorid dersom syren nøytraliseres. Dessuten vil bakvannet inneholde organiske klorforbindelser. I mindre utstrekning gjelder dette til og med for hypokloridblekningen og klordioksydblek-ningen. Common bleaching processes include, in the production of completely bleached pulps (whiteness = 88% MGO), one or two chlorination steps with elemental chlorine, and in most cases also one or two hypochlorite steps and one or two chlorine dioxide steps. In the chlorination step, where 4-8% CI2 calculated on the amount of pulp is usually used, large amounts of hydrochloric acid are formed, which means that the tailwater contains large amounts of this acid or sodium chloride if the acid is neutralized. The waste water will also contain organic chlorine compounds. To a lesser extent, this even applies to hypochlorite bleaching and chlorine dioxide bleaching.
Disse organiske stoffer og fremfor alt de organiske stoffer som løses opp under blekingen av massen, betyr en vesentlig belastning på de vassdrag og sjøer som bakvannet slip-pes ut i. Forøvrig er klorholdige væsker sterkt korrosive og vil skape store vansker i et gjenvinningssystem. These organic substances and, above all, the organic substances that are dissolved during the bleaching of the pulp, mean a significant burden on the waterways and lakes into which the waste water is discharged. Furthermore, chlorine-containing liquids are highly corrosive and will create major difficulties in a recycling system.
I denne forbindelse har man strebet etter en blekeprosess hvor klorblekningstrinnet blir erstattet med et oksygen-bleketrinn. In this connection, efforts have been made for a bleaching process where the chlorine bleaching step is replaced by an oxygen bleaching step.
Imidlertid er der til nå ikke kjent noen fremgangsmåte ved hvilken man gjennom anvendelse av oksygen kan unngå bruken av klorholdige blekemidler (klordioksyd) for å oppnå helblekte kvaliteter. However, until now no method is known by which, through the use of oxygen, the use of chlorine-containing bleaching agents (chlorine dioxide) can be avoided in order to achieve fully bleached qualities.
Som eksempel på konvensjonelle blekesekvenser kan føl-gende behandlingstrinn anføres: C/E/H, C/E/H/E/H, C/E/H/H, C/E/H/D, C/E/D/E/D, C/E/H/D/P, C/E/H/D/E/D, C/E/H/E/D og As an example of conventional bleaching sequences, the following treatment steps can be mentioned: C/E/H, C/E/H/E/H, C/E/H/H, C/E/H/D, C/E/D/ E/D, C/E/H/D/P, C/E/H/D/E/D, C/E/H/E/D and
C/E/H/D/E/H. C/E/H/D/E/H.
I den senere tid har man forsøkt å redusere mengden klorholdige blekemidler ved å erstatte klor (C) med oksygen (C^);men fortsatt må man bruke klordioksyd for å oppnå helblekte kvaliteter. Eksempler på slike behandlingssekvenser er som følger: In recent times, attempts have been made to reduce the amount of chlorine-containing bleaching agents by replacing chlorine (C) with oxygen (C^), but chlorine dioxide must still be used to achieve fully bleached qualities. Examples of such treatment sequences are as follows:
A/02/D/E/D, 02/D/E/D, 02/D/E/D, A/02/D/P/D. A/02/D/E/D, 02/D/E/D, 02/D/E/D, A/02/D/P/D.
I de ovennevnte sekvenser betyr C: klor, E: alkali, In the above sequences, C means chlorine, E means alkali,
H: hypoklorit, D: klordioksyd, P: peroksyd, 02: oksygen, H: hypochlorite, D: chlorine dioxide, P: peroxide, 02: oxygen,
A: syrevask, Z: ozon. A: acid wash, Z: ozone.
Fra SE-PS 405 130 er der kjent en 4- til 5-trinns From SE-PS 405 130, a 4- to 5-speed is known
klorfri blekeprosess med avvekslende bruk av peroksyd og per-syre. En slik prosess er imidlertid meget kostbar med dagens priser på de kjemikalier som inngår i prosessen, og torde derfor neppe finne praktisk anvendelse. chlorine-free bleaching process with alternating use of peroxide and per-acid. However, such a process is very expensive at today's prices for the chemicals included in the process, and is therefore unlikely to find practical use.
En hensikt med den foreliggende oppfinnelse går derfor ut på å gi anvisning på en fremgangsmåte til bleking av celluloseholdige masser uten bruk av klorholdige blekemidler, slik at man unngår de korrosjonsproblemer og miljøbelastninger som slike blekeprosesser fører med seg. One purpose of the present invention is therefore to provide instructions for a method for bleaching cellulose-containing masses without the use of chlorine-containing bleaching agents, so that the corrosion problems and environmental stress that such bleaching processes bring with them are avoided.
Fra NO-PS 115 279 er der kjent en fremgangsmåte til å øke en masses lyshet og lyshetens stabilitet mot belysning, idet massen behandles med en blanding av ozon/oksygen eller pzon/luft. Ifølge den kjente fremgangsmåte blir imidlertid massen tørket fra et organisk løsningsmiddel, dvs. under be-handlingen er massen oppslemmet i et organisk oppløsningsmid-del. Ved den foreliggende oppfinnelse er det tale om en fremgangsmåte hvor massen til stadighet er oppløst i vann, og hvor tørrstoffinnholdet i det minste er større enn 15%. From NO-PS 115 279 there is known a method for increasing the lightness of a mass and the stability of the lightness against illumination, the mass being treated with a mixture of ozone/oxygen or pzone/air. According to the known method, however, the mass is dried from an organic solvent, i.e. during the treatment the mass is suspended in an organic solvent. In the present invention, it is a process where the mass is constantly dissolved in water, and where the dry matter content is at least greater than 15%.
Videre er der fra SE-PS 373 396 kjent en fremgangsmåte til bleking og delignifisering av celluloseholdig materiale i en alkalisk oppløsning, hvilket i forbindelse med vanlig peroksydbleking tilsier at pH-verdien holdes på ca. 9-10. Ved den foreliggende oppfinnelse blir blekingen utført i et surt miljø, dvs. med en pH mindre eller lik 7. Med andre ord går fremgangsmåten ifølge oppfinnelsen ut på en ozonbehandling i surt miljø både i første og annet trinn. Furthermore, from SE-PS 373 396 a method for bleaching and delignification of cellulose-containing material in an alkaline solution is known, which in connection with ordinary peroxide bleaching means that the pH value is kept at approx. 9-10. In the present invention, the bleaching is carried out in an acidic environment, i.e. with a pH less than or equal to 7. In other words, the method according to the invention involves an ozone treatment in an acidic environment in both the first and second stages.
Således vedrører den foreliggende oppfinnelse en fremgangsmåte til bleking av oksygendelignifiserte celluloseholdige masser med ozon i et surt miljø og peroksyd, idet ozonbehandlingen finner sted i to trinn, hvilken fremgangsmåte foruten å være fri for de ovennevnte ulemper også kan inngå direkte i et eksisterende gjenvinningssystem. Thus, the present invention relates to a method for bleaching oxygen-delignified cellulosic masses with ozone in an acidic environment and peroxide, the ozone treatment taking place in two stages, which method, besides being free of the above-mentioned disadvantages, can also be incorporated directly into an existing recycling system.
Fremgangsmåten ifølge oppfinnelsen erkarakterisert vedThe method according to the invention is characterized by
at der i det første trinn foretas en ozonbehandling med samtidig eller etterfølgende peroksydbehandling (ZP), hvoretter massen underkastes et mellomliggende vasketrinn for pH-justering, awanning/pressing og fluffing, hvoretter massen i det annet trinn ozon- og peroksydbehandles (ZP), og at 55 - 85% that in the first step an ozone treatment is carried out with simultaneous or subsequent peroxide treatment (ZP), after which the pulp is subjected to an intermediate washing step for pH adjustment, dewatering/pressing and fluffing, after which the pulp is ozone and peroxide treated (ZP) in the second step, and that 55 - 85%
av de totale kjemikaliekvanta, dvs. ozon og peroksyd som benyttes i de to bleketrinn, tilsettes i første trinn, samtidig som der benyttes en total mengde ozon som ikke er større enn 1 %. of the total amount of chemicals, i.e. ozone and peroxide used in the two bleaching stages, is added in the first stage, while a total amount of ozone that is not greater than 1% is used.
Ved fremgangsmåten ifølge den foreliggende oppfinnelse oppnås der en høy SCAN-lyshet ved bruk av minimale mengder kjemikalier, dvs. minimale mengder ozon og peroksyd, samtidig som styrkeegenskapene for den ferdig blekede masse ikke redu-seres vesentlig i forhold til styrkeegenskapene den ville ha hatt uten å ha gjennomgått en blekeprosess. With the method according to the present invention, a high SCAN brightness is achieved by using minimal amounts of chemicals, i.e. minimal amounts of ozone and peroxide, while at the same time the strength properties of the finished bleached mass are not significantly reduced in relation to the strength properties it would have had without having undergone a bleaching process.
I magasinet Pulpand Paper Mag. Can. Vol. 75 No. 4. T153 In the magazine Pulpand Paper Mag. Can. Vol. 75 No. 4. T153
(1974) er der i en artikkel av N. Soteland beskrevet en fremgangsmåte ved ozon- og peroksydbleking som danner en forløper til den foreliggende oppfinnelse. Den kjente fremgangsmåte gir imidlertid kvalitetsmessig ikke tilfredsstillende resul-tater på flere massetyper. Dette skyldes de store kjemika-liemengder (ozon) som måtte benyttes for å få tilstrekkelig lyshet, dvs. helblekte kvaliteter, og disse store mengder kjemikalier førte til en uønsket stor styrkereduksjon hos cellulosemassen. (1974) there, in an article by N. Soteland, a method by ozone and peroxide bleaching is described which forms a precursor to the present invention. However, the known method does not give satisfactory results in terms of quality on several pulp types. This is due to the large amounts of chemicals (ozone) that had to be used to obtain sufficient lightness, i.e. fully bleached qualities, and these large amounts of chemicals led to an unwanted large reduction in the strength of the cellulose pulp.
Ved den foreliggende oppfinnelse oppnår man imidlertid helblekte massekvaliteter med tilfredsstillende styrkeegen-skaper. Et ytterligere særtrekk ved fremgangsmåten ifølge oppfinnelsen går ut på at massen oksygendelignifiseres til et kappatall i området 15-5 før bleking med ozon og peroksyd. With the present invention, however, completely bleached pulp qualities with satisfactory strength properties are obtained. A further distinctive feature of the method according to the invention is that the pulp is oxygen delignified to a kappa number in the range of 15-5 before bleaching with ozone and peroxide.
Oppfinnelsen vil i det følgende bli nærmere beskrevet under henvisning til tegningen som er et generelt flytskjema for fremgangsmåten ifølge oppfinnelsen. In the following, the invention will be described in more detail with reference to the drawing, which is a general flow chart for the method according to the invention.
Som vist på tegningen blir kokt og vasket celluloseholdig masse tilført et oksygendelignifiseringstrinn 1 hvor massen på kjent måte oksygendelignifiseres til et kappatall i området 15 - 5. As shown in the drawing, cooked and washed cellulosic pulp is fed to an oxygen delignification step 1 where the pulp is oxygen delignified in a known manner to a kappa number in the range 15 - 5.
Etter (^-trinnet tilføres massen som nå er alkalisk, After the (^-step) the mass, which is now alkaline, is added,
til et trinn 2 hvor massen vaskes, avvannes og fluffes. Den kombinerte vask og pH-justering av massen er symbolisert ved den mindre blokk 2a, idet massen her får sin pH-verdi justert til mindre eller lik 7. For sulfatmasser kan dette fordelak-tig utføres med svovelsyre. For sulfittmasser benyttes der sure kondensater fra selve sulfittkokingen. Massen underkastes vasking for fjerning av de oksygerte ligninforbindelser fra C^-trinnet. to a stage 2 where the mass is washed, dewatered and fluffed. The combined washing and pH adjustment of the mass is symbolized by the smaller block 2a, as the mass here has its pH value adjusted to less than or equal to 7. For sulphate masses, this can advantageously be carried out with sulfuric acid. For sulphite masses, acidic condensates from the sulphite boiling itself are used. The pulp is subjected to washing to remove the oxygenated lignin compounds from the C₂ stage.
Blokken merket 2b symboliserer avvanning av massen til et tørrstoffinnhold på ca. 25 - 60%, fortrinnsvis mellom 30 - 45%. The block marked 2b symbolizes the dewatering of the mass to a dry matter content of approx. 25 - 60%, preferably between 30 - 45%.
Blokken 2c anskueliggjør fluffetrinnet, idet massen her meddeles en finfordelt og luftig form for derigjennom å oppnå størst mulig spesifikk overflate for gassreaksjon. Block 2c illustrates the fluffing stage, as the mass is here given a finely divided and airy form in order to achieve the largest possible specific surface area for gas reaction.
Den fluffede masse behandles deretter med ozon i en ozon-reaktor 3, fortrinnsvis av den type som er beskrevet i norsk patentskrift nr. 137 651, hvoretter den ozonbehandlede masse behandles med alkalisk blekevæske (NaOH, Yi^ O^ i DTPA) i en underliggende høykonsistens-modningsreaktor, fortrinnsvis av den type som er beskrevet i norks patentskrift nr. 140 771. The fluffed pulp is then treated with ozone in an ozone reactor 3, preferably of the type described in Norwegian patent document no. 137 651, after which the ozone-treated pulp is treated with alkaline bleaching liquid (NaOH, Yi^ O^ in DTPA) in an underlying high-consistency ripening reactor, preferably of the type described in Nork's patent document No. 140,771.
Den ozon- og peroksydbehandlede masse blir deretter ført til et vaske- og avvanningstrinn 4 hvor blokken 4a indikerer vasking og pH-justering. pH-justeringen kan utføres ved tilsetting av svovelsyre (I^SO^) i vaskevannet, idet dette medfører en vinning av 2 - 3 lyshetsenheter. The ozone- and peroxide-treated pulp is then taken to a washing and dewatering step 4 where block 4a indicates washing and pH adjustment. The pH adjustment can be carried out by adding sulfuric acid (I^SO^) to the wash water, as this results in a gain of 2 - 3 lightness units.
Blokken 4b i trinnet 4 indikerer awanning/pressing til fortrinnsvis 30 - 45% TS av den vaskede og pH-justerte masse, som etter avvanning fluffes til en lett og luftig konsistens. Block 4b in step 4 indicates dewatering/pressing to preferably 30 - 45% TS of the washed and pH-adjusted pulp, which after dewatering is fluffed to a light and airy consistency.
På tegningen indikerer 5 ozon- og peroksydbehandlings-trinn nr. 2, som er av samme type som det beskrevet i forbindelse med trinn 3 ovenfor. 55 - 85% av de totale kjemikaliekvanta tilsettes i trinn 3 mens resten av kjemikaliene, dvs. 45 - 15% tilsettes ozon-og peroksydbehandlingstrinnet 5. In the drawing, 5 indicates ozone and peroxide treatment step no. 2, which is of the same type as that described in connection with step 3 above. 55 - 85% of the total chemical quantities are added in step 3, while the rest of the chemicals, i.e. 45 - 15%, are added in the ozone and peroxide treatment step 5.
EKSEMPLER: EXAMPLES:
Eksempel 1 Example 1
En oksygendelignifisert sulfatmasse av eukalyptus med kappatall 7 og viskositet 850 dm 3/kg presses til 40% tørr-stoff, fluffes og ozonbehandles med 0,4% 0^. Straks etter ozonering får massen tilsatt en væske bestående av vann + NaOH + + DTPA (dietylentriaminpentaasetat), slik at konsi-stensen blir 25%, og slik at mengdene kjemikalier regnet i forhold til massen blir henholdsvis 0,6%, 0,2% og 0,2%. An oxygen-delignified sulphate mass of eucalyptus with a kappa number of 7 and a viscosity of 850 dm 3 /kg is pressed to 40% dry matter, fluffed and ozone-treated with 0.4% 0^. Immediately after ozonation, a liquid consisting of water + NaOH + + DTPA (diethylene triamine pentaacetate) is added to the mass, so that the consistency becomes 25%, and so that the amounts of chemicals calculated in relation to the mass are respectively 0.6%, 0.2% and 0.2%.
Med denne blanding behandles massen i en time ved 90°C. Deretter presses massen, pH-justeres til 2 med svovelsyre og ozonbehandles på nytt med 0,2% O^. With this mixture, the mass is treated for one hour at 90°C. The mass is then pressed, pH-adjusted to 2 with sulfuric acid and ozone-treated again with 0.2% O^.
Etter ozonering tilsettes massen en væske bestående av avpresset blekevæske fra første trinns peroksydbleking pluss NaOH + H202 + DTPA, slik at kjemikaliemengdene beregnet på massen blir henholdsvis 0,4%, 0,1% og 0,1%. After ozonation, a liquid consisting of squeezed bleach liquid from the first stage of peroxide bleaching plus NaOH + H202 + DTPA is added to the pulp, so that the amounts of chemicals calculated for the pulp are respectively 0.4%, 0.1% and 0.1%.
Etter en behandlingstid på 1 time ved.90°C blir massen vasket og pH-regulert med S02~vann. Resultatene ses i tabell After a treatment time of 1 hour at 90°C, the mass is washed and pH-regulated with SO2 water. The results are shown in the table
I. IN.
Eksempel 2 Example 2
En oksygendelignifisert sulfatmasse av barved med kappatall 10 og viskositet 800 dm^/kg behandles som i eksempel 1 under anvendelse av 0,4% 0^i første ozontrinn og med henholdsvis 1,4% NaOH, 0,8% H202 og 0,2%DTPA i den påføglende alka-liske peroksydbehandling. An oxygen delignified sulphate mass of softwood with a kappa number of 10 and a viscosity of 800 dm^/kg is treated as in example 1 using 0.4% O^ in the first ozone stage and with respectively 1.4% NaOH, 0.8% H202 and 0.2 %DTPA in the subsequent alkaline peroxide treatment.
Annet trinns behandling består av 0,2% 03, 0,6% NaOH, 0,2% H202 og 0,1% DTPA. Second stage treatment consists of 0.2% O 3 , 0.6% NaOH, 0.2% H 2 O 2 and 0.1% DTPA.
Resultat ses i tabell I. Results can be seen in table I.
Eksempel 3 Example 3
En sulfittmasse av furu oksygendelignifisert med Mg(OH)2som base i oksygentrinnet og med kappatall 5 og viskositet 780 dm<3>/kg behandles som i eksempel 1. I første trinn anvendes 0,3% 03, 0,5% NaOH, 0,2% H202 og 0,2% DTPA. A sulphite mass of pine oxygen delignified with Mg(OH)2 as a base in the oxygen stage and with a kappa number of 5 and a viscosity of 780 dm<3>/kg is treated as in example 1. In the first stage, 0.3% 03, 0.5% NaOH, 0 .2% H 2 O 2 and 0.2% DTPA.
I annet trinn anvendes 0,2% 03, 0,3% NaOH, 0,1% H202In the second step, 0.2% O3, 0.3% NaOH, 0.1% H202 are used
og 0,1% DTPA. and 0.1% DTPA.
Resultatene ses i tabell I. The results can be seen in table I.
Claims (2)
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NO781190A NO144711C (en) | 1978-04-04 | 1978-04-04 | PROCEDURE FOR BLACKING OXYGEN-EQUIVALIZED CELLULOSE-containing OZONE |
| FI791056A FI68097C (en) | 1978-04-04 | 1979-03-29 | FOERFARANDE FOER BLEKNING AV EN GENOM OXIDERING DELIGNED CELLULOSAMASE WITH OZONE |
| SE7902901A SE439508B (en) | 1978-04-04 | 1979-04-02 | SET FOR BLACKING OF WATER SLIPED OXYGEN-SIGNIFIED, CELLULOSA-SUBSTANCES |
| CA000324788A CA1119360A (en) | 1978-04-04 | 1979-04-03 | Method for bleaching oxygen delignified cellulose-containing pulp with ozone |
| US06/400,115 US4450044A (en) | 1978-04-04 | 1982-07-19 | Method for bleaching oxygen delignified cellulose-containing pulp with ozone and peroxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NO781190A NO144711C (en) | 1978-04-04 | 1978-04-04 | PROCEDURE FOR BLACKING OXYGEN-EQUIVALIZED CELLULOSE-containing OZONE |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| NO781190L NO781190L (en) | 1979-10-05 |
| NO144711B true NO144711B (en) | 1981-07-13 |
| NO144711C NO144711C (en) | 1981-10-21 |
Family
ID=19884138
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO781190A NO144711C (en) | 1978-04-04 | 1978-04-04 | PROCEDURE FOR BLACKING OXYGEN-EQUIVALIZED CELLULOSE-containing OZONE |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US4450044A (en) |
| CA (1) | CA1119360A (en) |
| FI (1) | FI68097C (en) |
| NO (1) | NO144711C (en) |
| SE (1) | SE439508B (en) |
Families Citing this family (38)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE452346C (en) * | 1982-12-17 | 1990-03-26 | Sunds Defibrator | PROCEDURES FOR PEROXID WHITING OF LIGNOCELLULOSALLY MATERIAL IN TWO STEPS |
| US5181989A (en) * | 1990-10-26 | 1993-01-26 | Union Camp Patent Holdings, Inc. | Reactor for bleaching high consistency pulp with ozone |
| US5085734A (en) * | 1989-02-15 | 1992-02-04 | Union Camp Patent Holding, Inc. | Methods of high consistency oxygen delignification using a low consistency alkali pretreatment |
| US5173153A (en) * | 1991-01-03 | 1992-12-22 | Union Camp Patent Holding, Inc. | Process for enhanced oxygen delignification using high consistency and a split alkali addition |
| US5409570A (en) * | 1989-02-15 | 1995-04-25 | Union Camp Patent Holding, Inc. | Process for ozone bleaching of oxygen delignified pulp while conveying the pulp through a reaction zone |
| US5188708A (en) * | 1989-02-15 | 1993-02-23 | Union Camp Patent Holding, Inc. | Process for high consistency oxygen delignification followed by ozone relignification |
| US5472572A (en) * | 1990-10-26 | 1995-12-05 | Union Camp Patent Holding, Inc. | Reactor for bleaching high consistency pulp with ozone |
| US5211811A (en) * | 1989-02-15 | 1993-05-18 | Union Camp Patent Holding, Inc. | Process for high consistency oxygen delignification of alkaline treated pulp followed by ozone delignification |
| US5217574A (en) * | 1989-02-15 | 1993-06-08 | Union Camp Patent Holdings Inc. | Process for oxygen delignifying high consistency pulp by removing and recycling pressate from alkaline pulp |
| US5525195A (en) * | 1989-02-15 | 1996-06-11 | Union Camp Patent Holding, Inc. | Process for high consistency delignification using a low consistency alkali pretreatment |
| DE69016123T2 (en) * | 1989-08-02 | 1995-05-24 | Canon Kk | Image processing device. |
| US5164044A (en) * | 1990-05-17 | 1992-11-17 | Union Camp Patent Holding, Inc. | Environmentally improved process for bleaching lignocellulosic materials with ozone |
| US5164043A (en) * | 1990-05-17 | 1992-11-17 | Union Camp Patent Holding, Inc. | Environmentally improved process for bleaching lignocellulosic materials with ozone |
| US5441603A (en) * | 1990-05-17 | 1995-08-15 | Union Camp Patent Holding, Inc. | Method for chelation of pulp prior to ozone delignification |
| US5174861A (en) * | 1990-10-26 | 1992-12-29 | Union Camp Patent Holdings, Inc. | Method of bleaching high consistency pulp with ozone |
| US5520783A (en) * | 1990-10-26 | 1996-05-28 | Union Camp Patent Holding, Inc. | Apparatus for bleaching high consistency pulp with ozone |
| US5411634A (en) | 1991-04-30 | 1995-05-02 | Kamyr, Inc. | Medium consistency ozone bleaching |
| SE468355B (en) * | 1991-04-30 | 1992-12-21 | Eka Nobel Ab | CHEMISTRY OF CHEMICAL MASS THROUGH TREATMENT WITH COMPLEX PICTURES AND OZONE |
| AT400153B (en) * | 1991-05-02 | 1995-10-25 | Voest Alpine Ind Anlagen | METHOD FOR BLEACHING MATERIALS CONTAINING XYLAN AND LIGNOCELLULOSE |
| ATE156539T1 (en) * | 1991-05-24 | 1997-08-15 | Union Camp Patent Holding | TWO-STAGE REACTOR FOR BLEACHING PULP AND METHOD FOR BLEACHING WITH OZONE |
| NO912449L (en) * | 1991-06-24 | 1992-12-28 | Norske Stats Oljeselskap | MOVABLE PLATFORM FOR SEA. |
| ZA924351B (en) * | 1991-06-27 | 1993-03-31 | Ahlstroem Oy | Ozone bleaching process |
| US6039837A (en) * | 1991-09-17 | 2000-03-21 | Mo Och Domsjo Aktiebolag | Method of bleaching pulp with ozone wherein the acidity is maintained with an acid solution prepared by electrolysis or electrodialysis |
| SE500053C2 (en) * | 1991-09-17 | 1994-03-28 | Mo Och Domsjoe Ab | Ozone bleaching whereby the pulp is acidified with sulfuric acid produced by electrolysis |
| BE1006056A3 (en) * | 1992-07-06 | 1994-05-03 | Solvay Interox | Method of laundering of chemical pulp. |
| JPH08502556A (en) * | 1992-10-23 | 1996-03-19 | マクミラン ブローデル リミテッド | Improved ozone bleaching |
| FI93232C (en) * | 1993-03-03 | 1995-03-10 | Ahlstroem Oy | Process for bleaching pulp with chlorine-free chemicals |
| US6010594A (en) * | 1993-03-03 | 2000-01-04 | Ahlstrom Machinery Corporation | Method of bleaching pulp with chlorine-free chemicals wherein a complexing agent is added immediately after an ozone bleach stage |
| US5411635A (en) * | 1993-03-22 | 1995-05-02 | The Research Foundation Of State University Of New York | Ozone/peroxymonosulfate process for delignifying a lignocellulosic material |
| ES2111298T3 (en) * | 1993-04-06 | 1998-03-01 | Air Liquide | BLEACHING OF RECYCLED PASTE WITH OZONE AND HYDROGEN PEROXIDE. |
| SE501253C2 (en) * | 1993-06-08 | 1994-12-19 | Kvaerner Pulping Tech | Chlorine-free bleaching of chemical pulp |
| US5554259A (en) * | 1993-10-01 | 1996-09-10 | Union Camp Patent Holdings, Inc. | Reduction of salt scale precipitation by control of process stream Ph and salt concentration |
| US5688368A (en) * | 1993-12-10 | 1997-11-18 | Beloit Technologies, Inc. | Method for cooling and ozone bleaching wood pulp |
| US6210527B1 (en) | 1994-03-14 | 2001-04-03 | The Boc Group, Inc. | Pulp bleaching method wherein an ozone bleaching waste stream is scrubbed to form an oxygen containing stream |
| US5770010A (en) * | 1995-04-20 | 1998-06-23 | R-J Holding Company | Pulping process employing nascent oxygen |
| US20030131958A1 (en) * | 2001-11-30 | 2003-07-17 | Thomas Jaschinski | Use of ozone for increasing the wet strength of paper and nonwoven |
| EP1375734A1 (en) * | 2002-06-17 | 2004-01-02 | SCA Hygiene Products GmbH | Bleached, strong sulfite chemical pulp, a process for the production thereof and products derived therefrom |
| US7297225B2 (en) * | 2004-06-22 | 2007-11-20 | Georgia-Pacific Consumer Products Lp | Process for high temperature peroxide bleaching of pulp with cool discharge |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE373395B (en) * | 1972-12-19 | 1975-02-03 | Mo Och Domsjoe Ab | PROCEDURE FOR THE PRODUCTION OF CELLULOSA MASS WITH HIGH LIGHTNESS BY DISTRIBUTING WOOD WITH ACID GAS UNDER PRESSURE IN THE PRESENCE OF A COCK |
| US3966542A (en) * | 1974-09-20 | 1976-06-29 | General Signal Corporation | Multi-stage bleaching of pulp using successively lower power levels |
| NO137651C (en) * | 1975-10-31 | 1978-03-29 | Myrens Verksted As | PROCEDURE AND APPARATUS FOR CONTINUOUS TREATMENT OF FINDEL FIBER MATERIAL OR CELLULOSIZED MASS WITH GAS WITHOUT COVER. |
-
1978
- 1978-04-04 NO NO781190A patent/NO144711C/en unknown
-
1979
- 1979-03-29 FI FI791056A patent/FI68097C/en not_active IP Right Cessation
- 1979-04-02 SE SE7902901A patent/SE439508B/en not_active IP Right Cessation
- 1979-04-03 CA CA000324788A patent/CA1119360A/en not_active Expired
-
1982
- 1982-07-19 US US06/400,115 patent/US4450044A/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| FI791056A7 (en) | 1979-10-05 |
| CA1119360A (en) | 1982-03-09 |
| NO144711C (en) | 1981-10-21 |
| SE439508B (en) | 1985-06-17 |
| NO781190L (en) | 1979-10-05 |
| SE7902901L (en) | 1979-10-05 |
| FI68097C (en) | 1985-07-10 |
| US4450044A (en) | 1984-05-22 |
| FI68097B (en) | 1985-03-29 |
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